Integration of n-c4/n-c4=/bd separation system for on-purpose butadiene synthesis

ABSTRACT

A process for the production of butadiene is presented. The process combines the separation of butenes and butadienes extracted from a non-oxidated dehydrogenation process with the separation of butenes and butadienes from an oxidative dehydrogenation process to increase the butadiene yields and reduce the equipment for the recovery of a butadiene product.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a Continuation-in-Part of copending U.S. applicationSer. No. 14/749,059 filed Jun. 24, 2015, which application claimspriority from U.S. Provisional Application No. 62/018,973 filed Jun. 30,2014, now expired, the contents of which cited applications are herebyincorporated by reference in their entirety.

FIELD OF THE INVENTION

The present invention relates to a process for the production ofbutadiene. In particular, this is a process for the integration of abutadiene production process into a petrochemical plant.

BACKGROUND

The use of plastics and rubbers are widespread in today's world. Theproduction of these plastics and rubbers are from the polymerization ofmonomers which are generally produced from petroleum. The monomers aregenerated by the breakdown of larger molecules to smaller moleculeswhich can be modified. The monomers are then reacted to generate largermolecules comprising chains of the monomers. An important example ofthese monomers is light olefins, including ethylene and propylene, whichrepresent a large portion of the worldwide demand in the petrochemicalindustry. Light olefins, and other monomers, are used in the productionof numerous chemical products via polymerization, oligomerization,alkylation and other well-known chemical reactions. Producing largequantities of light olefin material in an economical manner, therefore,is a focus in the petrochemical industry. These monomers are essentialbuilding blocks for the modern petrochemical and chemical industries.The main source for these materials in present day refining is the steamcracking of petroleum feeds.

Another important monomer is butadiene. Butadiene is a basic chemicalcomponent for the production of a range of synthetic rubbers andpolymers, as well as the production of precursor chemicals for theproduction of other polymers. Examples include homopolymerized productssuch as polybutadiene rubber (PBR), or copolymerized butadiene withother monomers, such as styrene and acrylonitrile. Butadiene is alsoused in the production of resins such as acrylonitrile butadienestyrene.

Butadiene is typically recovered as a byproduct from the crackingprocess, wherein the cracking process produces light olefins such asethylene and propylene. With the increase in demand for rubbers andpolymers having the desired properties of these rubbers, an aim toimproving butadiene yields from materials in a petrochemical plant willimprove the plant economics.

SUMMARY

The present invention is for the improvement of the recovery ofbutadienes through a more efficient utilization of equipment in theproduction process.

A first embodiment of the invention is a process for the recovery ofbutadiene, comprising passing a first feedstream comprising n-butane toa dehydrogenation unit to generate a first butene process streamcomprising n-butene; passing the first n-butene process stream to abutane extraction column to generate a butane overhead stream and afirst n-butene stream, wherein the butane extraction column is operatedto recover the n-butenes in the first butene stream; passing the firstn-butene process stream to a butene extraction column to generate anoverhead stream comprising n-butene, and a bottoms stream comprisingbutadiene passing the overhead stream to an oxydehydrogenation unit togenerate a second process stream comprising n-butene and butadiene;passing the second process stream to a butene extraction column togenerate an overhead stream comprising n-butene, and a bottoms streamcomprising butadiene; passing a feedstream derived from an FCC or anMTO/OTO process to the butane extraction column, to the buteneextraction column, or to both columns; and passing the bottoms stream toa butadiene recovery unit to generate a butadiene stream.

A second embodiment of the invention is a process for the recovery ofbutadiene, comprising, passing a first feedstream comprising n-butane toa dehydrogenation unit to generate a first butene process streamcomprising n-butene; passing the first n-butene process stream to abutane extraction column to generate a butane overhead stream and afirst n-butene stream, wherein the butane extraction column is operatedto recover the n-butenes in the first butene stream; passing the butaneoverhead stream to a light gas separation unit to generate a vapor phasestream comprising hydrogen, and a liquid phase stream comprisingn-butane; passing at least a portion of the stream comprising hydrogenand at least a portion of the liquid phase stream to the dehydrogenationunit; passing the first n-butene process stream to a butene extractioncolumn to generate an overhead stream comprising n-butene, and a bottomsstream comprising butadiene; passing the overhead stream to anoxydehydrogenation unit to generate a second process stream comprisingn-butene and butadiene; passing the second process stream to a buteneextraction column to generate an overhead stream comprising n-butene,and a bottoms stream comprising butadiene; and passing the bottomsstream to a butadiene recovery unit to generate a butadiene stream.

A third embodiment of the invention is a process for the recovery ofbutadiene, comprising, passing a first feedstream comprising n-butane toa dehydrogenation unit to generate a first butene process streamcomprising n-butene; passing the first n-butene process stream to abutane extraction column to generate a butane overhead stream and afirst n-butene stream, wherein the butane extraction column is operatedto recover the n-butenes in the first butene stream; passing the firstn-butene process stream to a butene extraction column to generate anoverhead stream comprising n-butene, and a bottoms stream comprisingbutadiene; passing the overhead stream to a light gas separation unit togenerate a vapor phase stream comprising hydrogen, and a liquid phasestream comprising n-butene; passing at least a portion of the streamcomprising hydrogen and at least a portion of the liquid phase stream toan oxydehydrogenation unit; passing a second feedstream comprisingn-butene to the oxydehydrogenation unit to generate a second processstream comprising n-butene and butadiene; passing the second processstream to the butene extraction column; and passing the bottoms streamcomprising butadiene to a butadiene recovery unit to generate abutadiene stream.

Other objects, advantages and applications of the present invention willbecome apparent to those skilled in the art from the following detaileddescription and drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is the flow scheme of the present invention tying the productionof butenes and butadienes together.

FIG. 2 is a second embodiment of the flow scheme of the presentinvention tying the production of butenes and butadienes together.

DETAILED DESCRIPTION

The present process solves a problem associated with the heating ofbutadiene by integrating the extractive solvent system. In theproduction of butadiene from an on purpose butadiene synthesis processbeginning with butane, there is a separation step in between thenon-oxidative dehydrogenation of butane to generate butene and the stepof oxidative dehydrogenation of butenes to generate butadiene. This isto increase the concentration of butenes to improve the economics ofbutadiene production. The non-oxidative dehydrogenation also generatessome butadienes, and it is less desirable to feed this to the oxidativedehydrogenation step. Therefore, a partial combination of the separationof butadiene step is desirable, removing butadienes from any feed to theoxidative dehydrogenation reactor.

In one embodiment, the process can be seen in the FIG. 1, and includespassing a first feedstream 8 to a dehydrogenation unit 10 to generate afirst stream 12 comprising n-butene. The first stream 12 can be passedto a first light gas separation unit 20 to generate a vapor phase stream22 comprising hydrogen, and a first butene stream 24 comprisingn-butene. The first butene stream 24 is passed to a butane extractioncolumn 30 to generate a butane overhead stream 32 and a first n-butenestream 34. The amount of n-butane removal would depend on the economicsof the extraction step to the overall process. Preferably, the economicsprovide for the butane extraction column 30 to be operated to remove atleast 90% of the n-butanes, and preferably 100%, from the first butenestream. Light gas separation units can comprise a variety of methods forseparation of a process stream. One example is a depropanizer, or afractionation column to separate C3 and lighter components from theprocess stream, and to have C4 components pass out as a bottoms stream.Other means of separation are known to those skilled in the art,including adsorption-separation systems and the like.

The first feedstream 8 can be a supplied n-butane stream from an outsidesource, or can be an enriched n-butane stream from a natural gas orother hydrocarbon source. The present invention is not intended to berestricted to such enriched sources of n-butane. In addition, thisprocess can apply to a non-purified feedstream comprising n-butane. Thenon-purified feedstream can be enriched prior to passage to thedehydrogenation unit 10, or can be passed to the dehydrogenation unit 10with an added separation process following the dehydrogenation. Lightgases are readily removed in the first light gas separation unit 20, anda second separation step can be included to separate C4s from heaviercomponents.

Optionally, the process includes passing a second feedstream 42,comprising n-butene, to an oxydehydrogenation unit 50 to generate anoxydehydro process stream 52 comprising n-butene and butadiene. Theoxydehydrogenation unit 50 also includes a source of steam and oxygen.The oxygen can be supplied from an air source. The oxydehydrogenationprocess stream 52 is passed to a second light gas separation unit 60 togenerate a second light gas stream 62, and an intermediate butadienestream 64. The second light gas stream 62 can comprise CO, CO2, N2 andother components. Purification can be performed with anadsorbent-separation system, or other appropriate separation system. Thefirst n-butene stream 34 and the intermediate butadiene stream 64 arepassed to a butene extraction column 70 to generate a butene extractionoverhead stream 72 comprising n-butene and a butene extraction bottomsstream 74 comprising butadiene. The butene extraction bottoms 74 ispassed to a butadiene recovery unit 100 to generate a butadiene stream102.

Preferably, the column is operated to recovery substantially all then-butanes for recycle and to limit the amount of n-butane passed throughthe process units and reaching the oxydehydrogenation unit 50.

The process can further include passing the butane overhead stream 32 tothe dehydrogenation unit 10. The process can further include passingrecycling hydrogen by passing the vapor phase stream 22 to thedehydrogenation unit 10.

In one embodiment, the first 20 and second 60 light gas separation unitscomprise cold-box condensing units. Butanes and butenes have moderateboiling points that are near the freezing point of water. Cooling a gasstream comprising butanes and butenes can be accomplished with a lowexpense cold-box technology. The gas can be first expanded to cool thegas, then passed through a heat exchanger that cools the expanded gas toa temperature below −15 C. The C4 hydrocarbons then condense whilelighter gases such as hydrogen and any carbon oxides remain in thegaseous phase. The cold-box condensing unit 20, 60 is operated at atemperature to sufficiently condense the C4 hydrocarbons. Different C4hydrocarbons condense at temperatures between 1° C. and −12° C. at oneatmosphere. The cold-box unit 20, 60 is preferably operated at atemperature below −15° C. The light gases, including hydrogen, arereadily separated from the C4 compounds at these temperatures.

The butane extraction column 30 is a solvent separation process for theseparation of olefins from paraffins, or butenes from butane. Anappropriate solvent is a solvent comprising a polar nitrogen compound,or a mixture of polar compounds. Examples of solvents, though notlimited to these, include n-methylpyrrolidone (NMP), dimethylformamide(DMF), dimethyl acetamide, and acetonitrile (ACN). A common extractivesolvent is NMP. The solvent separation process can include additionalfractionation units for recovering the solvent and recycling the solventto the butane extraction column 30.

The butadiene recovery unit 100 can comprise fractionation units andsolvent extraction columns. In one embodiment, the butene extractionbottoms 74, comprising butadiene and solvent, is passed to a rectifyingcolumn 80 to generate a rectifying overhead stream 82 comprising butene,a rectifying intermediate stream 84 comprising butadiene, and arectifying bottoms stream 86 comprising solvent. The rectifying bottomsstream 86 is passed to a degassing column 110 to generate a degassingcolumn overhead stream 112 and a bottoms stream 114 comprising recoveredsolvent for reuse. The degassing column overhead stream 112 is passed tothe rectifying column 80. The intermediate stream 84 is passed to abutadiene extraction column 90 to generate a butadiene extraction columnbottoms comprising solvent and n-butene, and a butadiene stream 102. Thebutadiene stream 102 can be further passed to a butadiene purificationunit.

The oxydehydrogenation unit 50 includes feeds of stream and an oxygencontaining gas, such as air, to the oxydehydrogenation unit. The buteneextraction column and the butadiene extraction column are also solventextraction systems and include the passing of a solvent to the buteneextraction column and the butadiene extraction.

In another embodiment, the invention comprises passing a first streamcomprising n-butane to a non-oxidative dehydrogenation reactor togenerate a second stream comprising n-butane and n-butene, and lightgases. The second stream is passed to a light gas separation unit, whichcools and compresses the light gases to be separated. The light gasesare generated as a vapor phase and comprise hydrogen. The light gasseparation unit can utilize cold box technology to condense the C4hydrocarbons, and generates a third, liquid phase, stream comprisingn-butane and n-butene. The third stream is passed to a butane extractioncolumn to generate a fourth stream comprising n-butane and a fifthstream comprising n-butene. The extraction column uses a solventseparation system, with a solvent passed to the extraction column topreferentially absorb the olefin. The fourth stream can be recycled backto the non-oxidative dehydrogenation reactor.

A sixth stream comprising n-butene, along with steam and air, is passedto an oxydehydrogenation reactor to generate a seventh stream comprisingbutadiene, n-butene and light gases, such as hydrogen. The seventhstream is passed to a light gas separation unit to generate a vaporphase comprising the light gases, and an eighth stream comprising thebutadiene and n-butene. The fifth and eighth streams are passed to abutene extraction column at different stages in the column to generate aninth stream comprising n-butene and a tenth stream comprisingbutadiene.

The combined butenes from the dehydrogenation reactor andoxydehydrogenation reactor are separated in the butene extraction columnand are recycled to the oxydehydrogenation reactor.

The bottoms from the butene extraction column, comprising mostlybutadiene and solvent is passed to a butadiene recovery unit. Thebutadiene recovery unit includes a rectifying column to strip outresidual butenes. The rectifying column further generates anintermediate stream comprising butadiene and a bottoms stream comprisingsolvent. The intermediate stream is passed to a butadiene extractioncolumn to generate a butadiene product stream and a bottoms streamcomprising solvent. The bottoms stream from the butadiene extractioncolumn is passed back to the rectifying column.

The bottoms stream from the rectifying column is passed to a degassingcolumn for recovering solvent. The degassing column generates anoverhead stream comprising butadiene and is passed back to therectifying column to be recovered in the butadiene extraction column.The degassing column generates a bottoms stream comprising recoveredsolvent, which is recycled to the extraction columns for reuse.

In one embodiment, a feedstream which contains hydrocarbons with fourcarbon atoms where the feedstream is derived from a fluidized catalyticcracking (FCC) process or an oxygenate to olefin (OTO) process such as amethanol to olefin (MTO) process is introduced to the butane extractioncolumn, to the butene extraction column, or to both columns. In oneembodiment the feedstream derived from an FCC process is introduced tothe butane extraction column. In another embodiment the feedstreamderived from an OTO process is introduced into the butene extractioncolumn.

Turning to FIG. 2, another embodiment of the invention is shown wherethe first 220 and second 260 light gas separation units are located onthe overhead stream 32 of the butane extraction column 30 and on theoverhead stream 72 of the butene extraction column 70, respectively. Inone embodiment, the first 220 and second 260 light gas separation unitscomprise cold-box condensing units. Butanes and butenes have moderateboiling points that are near the freezing point of water. Cooling a gasstream comprising butanes and butenes can be accomplished with a lowexpense cold-box technology. The gas can be first expanded to cool thegas, then passed through a heat exchanger that cools the expanded gas toa temperature below −15° C. The C4 hydrocarbons then condense whilelighter gases such as hydrogen and any carbon oxides remain in thegaseous phase. The cold-box condensing units 220, 260 are operated at atemperature to sufficiently condense the C4hydrocarbons. Different C4hydrocarbons condense at temperatures between 1° C. and −12° C. at oneatmosphere. The cold-box units 220, 260 are preferably operated at atemperature below −15° C. The light gases, including hydrogen, arereadily separated from the C4 compounds at these temperatures.

Overhead stream 32 can be passed to a first light gas separation unit220 to generate a vapor phase stream 222 comprising hydrogen, and abutene stream 224 comprising n-butene. At least a portion of streams 222and 224 are passed to the dehydrogenation unit 10. Overhead stream 72can be passed to a second light gas separation unit 260 to generate avapor phase stream 262 comprising hydrogen, and a butene stream 264comprising n-butene. At least a portion of streams 262 and 264 arepassed to the oxydehydrogenation unit 50.

In another embodiment, the process also involves measuring a firstparameter of the process and generating an electrical signal associatedwith the first parameter. The electrical signal associated with thefirst parameter is transmitted to a processer which generates a secondelectrical signal. The second electrical signal is transmitted to acomponent of the process to affect an adjustment of a second parameterof the process in response to the second electrical signal. The firstand second parameters may be the same or different. The parameters maybe operating conditions or other parameters associated with the processsuch as maintenance parameters, safety parameters, catalyst relatedparameters, equipment related parameters, and the like. In anotherembodiment, the process further comprises connecting, electronically, atleast a first component of the process to at least a second component ofthe process wherein the connection incorporates at least one processor.The process may further comprise comprising sensing and collecting dataregarding the process and adjusting the process in response to thesensed and collected data.

Specific Embodiments

While the following is described in conjunction with specificembodiments, it will be understood that this description is intended toillustrate and not limit the scope of the preceding description and theappended claims.

A first embodiment of the invention is a process for the recovery ofbutadiene, comprising passing a first feedstream comprising n-butane toa dehydrogenation unit to generate a first butene process streamcomprising n-butene; passing the first n-butene process stream to abutane extraction column to generate a butane overhead stream and afirst n-butene stream, wherein the butane extraction column is operatedto recover the n-butenes in the first butene stream; passing the firstn-butene process stream to a butene extraction column to generate anoverhead stream comprising n-butene, and a bottoms stream comprisingbutadiene passing the overhead stream to an oxydehydrogenation unit togenerate a second process stream comprising n-butene and butadiene;passing the second process stream to a butene extraction column togenerate an overhead stream comprising n-butene, and a bottoms streamcomprising butadiene; passing at least one feedstream derived from anFCC process or from an OTO process to the butane extraction column, tothe butene extraction column, or to both the butane and buteneextraction columns; and passing the bottoms stream to a butadienerecovery unit to generate a butadiene stream. An embodiment of theinvention is one, any or all of prior embodiments in this paragraph upthrough the first embodiment in this paragraph further comprisingpassing a second feedstream comprising n-butene to an oxydehydrogenationunit to generate a second process stream comprising n-butene andbutadiene; and passing the second process stream to the buteneextraction column. An embodiment of the invention is one, any or all ofprior embodiments in this paragraph up through the first embodiment inthis paragraph further comprising passing the butadiene stream to abutadiene purification unit. An embodiment of the invention is one, anyor all of prior embodiments in this paragraph up through the firstembodiment in this paragraph further comprising passing the first buteneprocess stream to a light gas separation unit to generate a vapor phasestream comprising hydrogen, and a liquid phase stream comprisingn-butane and n-butene, wherein the light gas separation unit is acold-box separation unit; and passing the liquid phase stream to abutane extraction column to generate a butane overhead stream and thefirst n-butene process stream. An embodiment of the invention is one,any or all of prior embodiments in this paragraph up through the firstembodiment in this paragraph further comprising passing the butaneoverhead stream to the dehydrogenation unit. An embodiment of theinvention is one, any or all of prior embodiments in this paragraph upthrough the first embodiment in this paragraph further comprisingpassing a portion of the vapor phase stream to the dehydrogenation unit.An embodiment of the invention is one, any or all of prior embodimentsin this paragraph up through the first embodiment in this paragraphwherein the light gas separation unit is a cold-box separation unit tocondense the butane and butenes, while separating hydrogen and otherlight gases from the first process stream. An embodiment of theinvention is one, any or all of prior embodiments in this paragraph upthrough the first embodiment in this paragraph further comprisingpassing a solvent to the butane extraction column. An embodiment of theinvention is one, any or all of prior embodiments in this paragraph upthrough the first embodiment in this paragraph wherein the solvent isselected from the group consisting of n-methyl-2-pyrrolidone (NMP),dimethylformamide (DMF), acetonitrile (ACN), and mixtures thereof. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph whereinthe oxydehydrogenation unit generates an intermediate stream, furthercomprising passing the intermediate stream to a second light gasseparation unit to generate a second light gas stream and a secondintermediate stream comprising butadiene and n-butene; and passing thesecond intermediate stream to the butene extraction column. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph furthercomprising passing a solvent to the butene extraction column. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph furthercomprising passing steam and air to the oxydehydrogenation unit. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph whereinpassing the bottoms stream to the butadiene recovery unit comprisespassing the bottoms stream to a rectifying column to generate anoverhead stream, an intermediate stream comprising butadiene, and arectifying bottoms stream; passing the rectifying bottoms stream to adegassing column to generate a degassing column overhead stream an asolvent recovery bottoms stream; passing the degassing column overheadstream to the rectifying column; passing the intermediate stream to abutadiene extraction column to generate a butadiene extraction columnbottoms comprising solvent and n-butene, and the butadiene stream. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph furthercomprising passing a solvent to the butadiene extraction column. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the first embodiment in this paragraph furthercomprising measuring a first parameter of the process and generating anelectrical signal associated with the parameter; transmitting theelectrical signal to a processer and generating a second electricalsignal; transmitting the second electrical signal to a component of theprocess and adjusting a second parameter of the process in response tothe second electrical signal. An embodiment of the invention is one, anyor all of prior embodiments in this paragraph up through the firstembodiment in this paragraph further comprising connecting,electronically, at least a first component of the process to at least asecond component of the process wherein the connection incorporates atleast one processor. An embodiment of the invention is one, any or allof prior embodiments in this paragraph up through the first embodimentin this paragraph further comprising sensing and collecting dataregarding the process and adjusting the process in response to thesensed and collected data.

A second embodiment of the invention is a process for the recovery ofbutadiene, comprising passing a first stream comprising n-butane to adehydrogenation reactor to generate a second stream comprising n-butaneand n-butene; passing the second stream to a light gas separation unitto generate a vapor phase comprising hydrogen, and a third streamcomprising liquid n-butane and n-butene; passing the third stream to abutane extraction column to generate a fourth stream comprising n-butaneand a fifth stream comprising n-butene; passing the fifth stream to abutene extraction column; passing a sixth stream comprising n-butene toan oxydehydrogenation reactor to generate a seventh stream comprisingbutadiene and n-butene; passing the seventh stream to a second light gasseparation unit to generate a second vapor phase comprising light gases,and an eighth stream comprising butadiene and n-butene; and passing theeighth stream to the butene extraction column to generate a ninth streamcomprising n-butene, and a tenth stream comprising butadiene. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the second embodiment in this paragraphwherein the fifth stream and the eighth stream are passed to the buteneextraction column at different stages. An embodiment of the invention isone, any or all of prior embodiments in this paragraph up through thesecond embodiment in this paragraph further comprising passing the tenthstream to a rectifying column to generate an overhead stream anintermediate stream comprising butadiene and a bottoms stream comprisingsolvent; and passing the intermediate stream to a butadiene extractioncolumn to generate a butadiene product stream and a bottoms stream. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the second embodiment in this paragraphfurther comprising passing the butadiene extraction column bottomsstream to the rectifying column. An embodiment of the invention is one,any or all of prior embodiments in this paragraph up through the secondembodiment in this paragraph further comprising passing the rectifyingcolumn bottoms stream to a degassing column to generate a degassingcolumn overhead and a recovered solvent bottoms stream; and passing thedegassing column overhead stream to the rectifying column. An embodimentof the invention is one, any or all of prior embodiments in thisparagraph up through the second embodiment in this paragraph furthercomprising passing steam and air to the oxydehydrogenation reactor. Anembodiment of the invention is one, any or all of prior embodiments inthis paragraph up through the second embodiment in this paragraphwherein the extraction columns comprise passing a solvent to theextraction column.

While the invention has been described with what are presentlyconsidered the preferred embodiments, it is to be understood that theinvention is not limited to the disclosed embodiments, but it isintended to cover various modifications and equivalent arrangementsincluded within the scope of the appended claims.

1. A process for the recovery of butadiene, comprising: passing a firstfeedstream comprising n-butane to a dehydrogenation unit to generate afirst butene process stream comprising n-butene; passing the firstn-butene process stream to a butane extraction column to generate abutane overhead stream and a first n-butene stream, wherein the butaneextraction column is operated to recover the n-butenes in the firstbutene stream; passing the first n-butene process stream to a buteneextraction column to generate an overhead stream comprising n-butene,and a bottoms stream comprising butadiene; passing the overhead streamto an oxydehydrogenation unit to generate a second process streamcomprising n-butene and butadiene; passing the second process stream toa butene extraction column to generate an overhead stream comprisingn-butene, and a bottoms stream comprising butadiene; passing at leastone feedstream derived from an FCC process or from an OTO process to thebutane extraction column, to the butene extraction column, or to boththe butane and butene extraction columns; and passing the bottoms streamto a butadiene recovery unit to generate a butadiene stream.
 2. Theprocess of claim 1 further comprising: passing a second feedstreamcomprising n-butene to an oxydehydrogenation unit to generate a secondprocess stream comprising n-butene and butadiene; and passing the secondprocess stream to the butene extraction column.
 3. The process of claim1 further comprising: passing the first butene process stream to a lightgas separation unit to generate a vapor phase stream comprisinghydrogen, and a liquid phase stream comprising n-butane and n-butene;and passing the liquid phase stream to a butane extraction column togenerate a butane overhead stream and the first n-butene process stream.4. The process of claim 3 further comprising: passing the butaneoverhead stream to the dehydrogenation unit; and passing a portion ofthe vapor phase stream to the dehydrogenation unit.
 5. The process ofclaim 3 wherein the light gas separation unit is a cold-box separationunit to condense the butane and butenes, while separating hydrogen andother light gases from the first process stream.
 6. The process of claim1 further comprising passing a first solvent to the butane extractioncolumn and a second solvent to the butene extraction column wherein thefirst and second solvents are selected from the group consisting ofn-methyl-2-pyrrolidone (NMP), dimethylformamide (DMF), acetonitrile(ACN), and mixtures thereof.
 7. The process of claim 1 wherein theoxydehydrogenation unit generates an intermediate stream, furthercomprising: passing the intermediate stream to a second light gasseparation unit to generate a second light gas stream and a secondintermediate stream comprising butadiene and n-butene; and passing thesecond intermediate stream to the butene extraction column.
 8. Theprocess of claim 1 further comprising passing steam and air to theoxydehydrogenation unit.
 9. The process of claim 1 wherein passing thebottoms stream to the butadiene recovery unit comprises: passing thebottoms stream to a rectifying column to generate an overhead stream, anintermediate stream comprising butadiene, and a rectifying bottomsstream; passing the rectifying bottoms stream to a degassing column togenerate a degassing column overhead stream an a solvent recoverybottoms stream; passing the degassing column overhead stream to therectifying column; and passing the intermediate stream to a butadieneextraction column to generate a butadiene extraction column bottomscomprising solvent and n-butene, and the butadiene stream.
 10. Theprocess of claim 9 further comprising passing a solvent to the butadieneextraction column.
 11. The process of claim 1 further comprising:measuring a first parameter of the process and generating an electricalsignal associated with the parameter; transmitting the electrical signalto a processer and generating a second electrical signal; transmittingthe second electrical signal to a component of the process and adjustinga second parameter of the process in response to the second electricalsignal.
 12. The process of claim 1 further comprising connecting,electronically, at least a first component of the process to at least asecond component of the process wherein the connection incorporates atleast one processor.
 13. The process of claim 1 further comprisingsensing and collecting data regarding the process and adjusting theprocess in response to the sensed and collected data.
 14. The process ofclaim 1 wherein the feedstream derived from a FCC process is introducedto the butane extraction column.
 15. The process of claim 1 wherein thefeedstream derived from an OTO process is introduced to the buteneextraction column.
 16. A process for the recovery of butadiene,comprising: passing a first feedstream comprising n-butane to adehydrogenation unit to generate a first butene process streamcomprising n-butene; passing the first butene process stream to a butaneextraction column to generate a butane overhead stream and a firstbutene stream, wherein the butane extraction column is operated torecover the n-butenes in the first butene stream; passing the butaneoverhead stream to a light gas separation unit to generate a vapor phasestream comprising hydrogen, and a liquid phase stream comprisingn-butane; passing at least a portion of the stream comprising hydrogenand at least a portion of the liquid phase stream to the dehydrogenationunit; passing the first butene stream to a butene extraction column togenerate an overhead stream comprising butene, and a bottoms streamcomprising butadiene; passing the overhead stream comprising butene toan oxydehydrogenation unit to generate a second process streamcomprising butene and butadiene; passing the second process streamcomprising butene to the butene extraction column; and passing thebottoms stream to a butadiene recovery unit to generate a butadienestream.
 17. A process for the recovery of butadiene, comprising: passinga first feedstream comprising n-butane to a dehydrogenation unit togenerate a first butene process stream comprising n-butene; passing thefirst butene process stream to a butane extraction column to generate abutane overhead stream and a first butene stream, wherein the butaneextraction column is operated to recover the n-butenes in the firstbutene stream; passing the first butene stream to a butene extractioncolumn to generate an overhead stream comprising butene, and a bottomsstream comprising butadiene; passing the overhead stream comprisingbutene to a light gas separation unit to generate a vapor phase streamcomprising hydrogen, and a liquid phase stream comprising butene;passing at least a portion of the stream comprising hydrogen and atleast a portion of the liquid phase stream to an oxydehydrogenationunit; passing a second feedstream comprising n-butene to theoxydehydrogenation unit to generate a second process stream comprisingn-butene and butadiene; passing the second process stream to the buteneextraction column; and passing the bottoms stream comprising butadieneto a butadiene recovery unit to generate a butadiene stream.